EP2153879B1 - Séparation des gaz par condensation en plusieurs étapes - Google Patents

Séparation des gaz par condensation en plusieurs étapes Download PDF

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Publication number
EP2153879B1
EP2153879B1 EP08014024.7A EP08014024A EP2153879B1 EP 2153879 B1 EP2153879 B1 EP 2153879B1 EP 08014024 A EP08014024 A EP 08014024A EP 2153879 B1 EP2153879 B1 EP 2153879B1
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EP
European Patent Office
Prior art keywords
gas
gas component
pressure
liquefaction device
condensate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Not-in-force
Application number
EP08014024.7A
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German (de)
English (en)
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EP2153879A1 (fr
Inventor
Udo Tielcke
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens AG
Original Assignee
Siemens AG
Siemens Corp
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Publication date
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Priority to EP08014024.7A priority Critical patent/EP2153879B1/fr
Publication of EP2153879A1 publication Critical patent/EP2153879A1/fr
Application granted granted Critical
Publication of EP2153879B1 publication Critical patent/EP2153879B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0036—Multiple-effect condensation; Fractional condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention relates to the technical field of separating a gas from a gas mixture which, in addition to the type of gas to be separated off, has at least one further type of gas.
  • the present invention relates to the separation of non-condensable gases from a steam cycle.
  • CO2 carbon dioxide
  • a particularly advantageous combustion process from an energetic point of view is the so-called oxyfuel process.
  • this natural gas is burned with the main component methane CH4 with pure oxygen (02) in a high-temperature combustion chamber with the addition of pure water (H2O) as a temperature regulator.
  • H2O pure water
  • CO2 sequestration An effective method for reducing CO2 emissions is so-called CO2 sequestration.
  • This refers to the landfilling of CO2, which has been generated, for example, in gas-fired power plants as part of power generation by means of gas turbines.
  • Sequestration is part of the so-called CCS (Carbon Dioxide Capture and Storage Process) process for the low-carbon use of fossil fuels in power generation.
  • the CO2 from the combustion of fossil fuels is to be separated from the exhaust air of a power plant and then stored so that it does not get into the atmosphere and its negative greenhouse gas effects are not unfolding.
  • Geological formations such as oil deposits, natural gas deposits, saline aquifers and coal seams as well as storage in the deep sea are currently being discussed as potential CO2 storage sites.
  • it is important that CO2 in the liquid form is heavier than seawater and that CO2 does not mix with the waters of the deep sea. Trials in water depths of 3500 m have confirmed the correctness of the assumption.
  • the present invention has for its object to provide a method for separating a gas from a gas mixture, which allow an effective gas separation in the context of a large-scale application.
  • the method is based on the finding that the first gas, or the first gas component carbon dioxide, can be deposited in a particularly high purity by means of a two-stage condensation of the second gas or of the second gas component water. In the two described condensation processes, the second gas is largely converted into the liquid state of aggregation.
  • the intermediate gas mixture is forwarded automatically or at least with the assistance of it pressure difference.
  • the separation of the gases follows the regularities of the partial pressures of the individual gas components.
  • H2O is not or only very difficult to mix with CO2 and H2O in gaseous form has a significantly different dew point than other gases, such as CO2, argon or nitrogen oxides (NOx).
  • the second gas in the first liquefaction device which is also referred to below as the first condensate
  • the first condensate is removed by means of a pump.
  • the pumped-off first condensate can then optionally be used for other process steps, such as one in a heat exchanger or a regenerative desuperheater.
  • the second gas condensed in the second liquefying device which is also referred to below as the second condensate, can be removed by means of a pump.
  • the pumped-off second condensate can optionally also be used for other process steps such as heat exchange in a heat exchanger or a regenerative desuperheater. It is also possible to merge and thus share the first and second condensates.
  • the second gas may also be a vapor which, in addition to some gaseous components, also has liquid fractions already possibly condensed.
  • steam is a gas which is generally still in contact with the liquid phase.
  • the liquid phase can be distributed homogeneously or inhomogeneously in the corresponding gas volume.
  • the second gas may also be a composition of water and various other gases, such as NOx and argon, which have a significantly different dew point characteristic as compared to the dewpoint characteristic of the first gas.
  • gases such as NOx and argon
  • the gas separation process described has the advantage that it can be carried out cost-effectively in a large-scale plant.
  • the described method is particularly suitable for processes in which gas turbines such as gas expanders work in combination with conventional steam turbines in combination.
  • the prerequisite here is that the water vapor gas mixture in all phases of the water vapor gas relaxation in the turbine parts is always above the dew point of the gases, inter alia, to avoid corrosion of the atmospheric oxygen.
  • High temperature distances to the dew point line (s) of the individual gas components, Also in the pressure range far below the atmospheric pressure, are for effective gas separation of advantage.
  • the condensation of a part of the second gas and / or the condensation of at least one further part of the second gas takes place on a cooled surface.
  • the first pressure and the second pressure are lower than an ambient pressure.
  • the negative pressure relative to the assumed atmospheric pressure of the environment can be established via the suction effect of a connected gas compressor or a pump for the second gas or the residual gas mixture.
  • the gas flow control and the negative pressure generated thereby can be controlled via a gas pressure control station.
  • the corresponding pumps should be adjusted with regard to their suction so that preferably only liquid or the respective condensate and as little as possible of gaseous substances are withdrawn from the respective liquefaction device.
  • the method additionally comprises compressing the deposited first gas.
  • the first gas can be liquefied. If the first gas is at least in the gaseous phase harmful to the environment, then the volume of this substance can be significantly reduced by the described liquefaction and thus a disposal can be realized. Of course, care should be taken in such a high pressure supply that a required for maintaining the liquid phase minimum pressure is maintained.
  • the suction effect generated by the compressor should not be so great that that generated in the second liquefaction device second condensate is sucked in from a process space of the second liquefying device.
  • the gas mixture from a regenerative desuperheater is supplied to the first liquefying device.
  • the regenerative desuperheater which can work in particular according to the known principle of a heat exchanger, can be connected in particular downstream of a steam turbine or a gas turbine.
  • a steam turbine for example, the first condensate and / or the second condensate can be used.
  • the method additionally comprises (a) forwarding the separated first gas to a third liquefying device, wherein at least a part of the second gas adheres to the deposited first gas, (b) condensing at least a part of the second Gas in the third liquefier at a third pressure which is less than the second pressure, and (c) separating the first gas from the second gas condensed in the third liquefaction means.
  • the described third condensation has the advantage that the first gas can be deposited in an even greater purity.
  • the described gas separation process can also be carried out in more than three condensation stages, wherein the degree of purity of the separated gas, apart from undesirable pollution effects, typically increases with each condensation stage.
  • condensation stages in particular generated by compression and cooling, can also be used to separate more than one type of gas from a gas mixture of different gases.
  • process parameters such as in particular the temperature and the pressure of the individual condensation processes can be dependent be adjusted by the dew points of the remaining gases such that the best possible separation is already achieved with a single optimized for each gas condensation stage.
  • the second gas, gaseous water, which is chemically described by the formula H2O, may in particular be a water vapor. In its state of aggregation, this is generally as invisible as air.
  • the second condensate which is generated from the gaseous water in the first liquefaction device and / or in the second liquefaction device, can be supplied, for example, to a combustion process taking place in a gas turbine in order to avoid undesired overheating of the gas turbine or at least parts of the gas turbine.
  • This process, with which the gas turbine can be protected from damage, is also called spraying.
  • This cumshot is particularly in connection with the combustion of natural gas in the context of o. G. Oxyfuel process relevant.
  • the first gas to be separated is carbon dioxide (CO2), which can be produced by burning natural gas with almost 100% methane (CH4) with pure oxygen (02).
  • CO2 carbon dioxide
  • CH4 methane
  • pure oxygen pure oxygen
  • many natural gas deposits contain high amounts of nitrogen (N2) up to 25%, sulfur and / or argon.
  • N2 nitrogen
  • These components remain in separation processes as non-condensable gas components in possible forms such as NOx, ammonia, hydrogen sulfide and are separated together with the predominant proportion of carbon dioxide gas with.
  • the required purity of the gases or residual gas mixtures to be withdrawn from the various gas components can be achieved by known gas separation methods which are connected after the first compressor stage.
  • the method described has great environmental significance.
  • the mainly responsible for the so-called greenhouse effect CO2 which inevitably arises in the combustion of fossil fuels such as natural gas or petroleum, can be discarded from the combustion air, especially after liquefaction by means of a suitable compression disposed.
  • This disposal can also take place at great depths in the oceans at great depths or in natural gas or petroleum reservoirs, where there is such great pressure that the liquefied CO2 does not revert to the gaseous phase.
  • it is very important that liquefied CO2 is heavier than water so that it automatically sinks to the bottom of the sea.
  • the gas mixture is produced by combustion of oxyfuel.
  • combustion which takes place on the principle of a rocket drive, the gas to be burned oxygen is supplied.
  • high-efficiency combustion process which is represented by the chemical equation CH4 + 2 02 -> CO2 + 2 H2O
  • the oxyfuel process itself is a combustion process in which particularly high flame temperatures can be achieved. It is applicable to both gaseous and liquid and solid fuels.
  • solid fuels have to be converted into gas in a separate gasification process, similar to the known coal gasification process.
  • the fuel is to be converted into an exothermic process with pure oxygen with the addition of water, water vapor with definable carbon dioxide gas fractions, and other NOx gas fractions, argon gas fractions, and other gas fractions, depending on the fuel contaminants.
  • FIG. 1 shows a gas separation device 100.
  • the gas separation device 100 is connected downstream of a regenerative desuperheater 180.
  • the regenerative desuperheater 180 is in turn connected downstream of a water vapor or gas turbine, not shown, which is operated with the above-described fuel oxyfuel.
  • a gas mixture 110 is formed at the outlet of the steam or gas turbine or at the outlet of the regenerative desuperheater 180, which contains 111 carbon dioxide (CO2) as first gas and water vapor (H2O) as second gas 112.
  • CO2 carbon dioxide
  • H2O water vapor
  • this gas mixture 110 is supplied via a pipeline 185 to a first liquefying device 120.
  • the first liquefying device is a so-called steam condenser 120, which is also referred to below as the main cooler.
  • the main cooler 120 part of the water vapor condenses on a cooled surface 121.
  • the condensation process takes place at a working pressure p1.
  • the pressure p1 is less than an ambient air pressure p0.
  • the first condensate 112a is liquid water, which is supplied via an outlet opening 123 and via a pump 124 to a return line 182. How out FIG. 1 As can be seen, this return line opens into the regenerative desuperheater 180, where it can withdraw heat from the gas mixture 110 as part of a heat exchange process.
  • the at least slightly heated water 112a may be supplied to the combustion process of the oxyfuel in the gas turbine. As explained above, such spraying of the combustion process can serve to protect the steam or gas turbine from thermal damage by the high temperatures caused by the oxyfuel.
  • the resulting intermediate mixture 130 is supplied to a second liquefying device 140 via a connecting element 125 designed as a pipeline.
  • the second liquefying device is likewise a so-called steam condenser 140, which is also referred to below as the aftercooler.
  • the aftercooler 120 At least a portion of the water vapor remaining in the intermediate mixture 130 condenses again on a cooled surface 141.
  • the second condensation process takes place at a working pressure p 2.
  • the pressure p2 is smaller than the working pressure p1 within the main cooler 120, so that the intermediate mixture 130 is automatically transferred to the aftercooler 140 according to the course of the pressure gradient.
  • the second condensate 112b is again liquid water, which is supplied via an outlet opening 143 and via a pump 144 to the return line 182 already described above.
  • the carbon dioxide is supplied via a short pipe connection designed as a second connecting element 145 and an outlet opening 153 of a separation device 190.
  • the separation device is a compressor 190, with which the carbon dioxide is liquefied.
  • FIG. 2 shows in a cross-sectional view the in FIG. 1 illustrated gas separation device, which is now designated by the reference numeral 200.
  • the mixed gas of water vapor and carbon dioxide enters the main cooler 220 via the pipe 285.
  • a part of the water vapor condenses on the cooled surface 221 of a cooling block 221a.
  • the cooling block 221a has an inlet opening 222a and an outlet opening 222b for a cooling liquid.
  • the condensed water exits via an outlet opening 223.
  • this pneumatic connecting element has a continuously tapering in the flow direction cross-section. This taper is designed such that the intermediate mixture on the way from the main radiator 220 to the aftercooler 240 has an at least approximately constant flow velocity.
  • the cross-sectional area of the inlet nozzle of the aftercooler 240 is approximately 10-15% of the cross-sectional area of the outlet nozzle of the main cooler 220 in this embodiment. In this way, a flow resistance arises between the main cooler 220 and the aftercooler 240, so that 220 and 240 differ in the two coolers Working pressures are built.
  • the aftercooler also has a cooling block, which in FIG. 2 is provided with the reference numeral 241a.
  • the cooling block 241a there are also an inlet opening 242a and an outlet opening 242b for cooling liquid.
  • the liquid condensate generated in the aftercooler 240 can be removed.
  • the carbon dioxide still present in gaseous form, which has been effectively dried by the described two-stage condensation process, can be separated off. The subsequent liquefaction of the carbon dioxide is carried out as above in connection with FIG. 1 described with an in FIG. 2 not shown compressor.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

Claims (4)

  1. Procédé pour séparer un premier composant gazeux (111) d'un mélange gazeux (110) contenant, outre le premier composant gazeux (111), au moins encore un deuxième composant gazeux (112), le procédé comprenant
    • l'acheminement du mélange gazeux (110) jusqu'à un premier dispositif de liquéfaction (120),
    • la condensation d'une partie du deuxième composant gazeux (112) dans le premier dispositif de liquéfaction (120) à une première pression pour obtenir un premier condensat (112a), de sorte qu'il se forme un mélange gazeux intermédiaire (130) dans lequel la proportion du premier composant gazeux (111) est augmentée par rapport à la proportion du premier composant gazeux (111) dans le mélange gazeux d'origine (110) ;
    • le réacheminement du mélange gazeux intermédiaire (130) du premier dispositif de liquéfaction (120) jusqu'à un deuxième dispositif de liquéfaction (140),
    • la condensation au moins d'une autre partie du deuxième composant gazeux (112) dans le deuxième dispositif de liquéfaction (140) à une deuxième pression, inférieure à la première pression, pour obtenir un deuxième condensat (112b), et
    • la séparation du premier composant gazeux (111) du deuxième composant gazeux (112b) condensé dans le deuxième dispositif de liquéfaction (140),
    le premier condensat (112a) et/ou le deuxième condensat (112b) étant recyclé dans un désurchauffeur régénératif (180) pour extraire de la chaleur du mélange gazeux (110),
    le mélange gazeux étant acheminé du désurchauffeur régénératif (180) jusqu'au premier dispositif de liquéfaction (120),
    la deuxième pression étant inférieure à la pression ambiante,
    la première pression étant inférieure à la pression ambiante,
    le deuxième composant gazeux étant de l'eau à l'état gazeux (112),
    le premier composant gazeux (111) étant du dioxyde de carbone (CO2).
  2. Procédé selon la revendication précédente,
    la condensation d'une partie du deuxième composant gazeux (112) et/ou
    la condensation de l'au moins une autre partie du deuxième composant gazeux (112)
    s'effectuant sur une surface refroidie (121, 141).
  3. Procédé selon l'une des revendications précédentes, comprenant en outre
    • le réacheminement du premier composant gazeux séparé jusqu'à un troisième dispositif de liquéfaction, le premier composant gazeux séparé contenant au moins encore une partie du deuxième composant gazeux,
    • la condensation au moins encore d'une autre partie du deuxième composant gazeux dans le troisième dispositif de liquéfaction à une troisième pression, inférieure à la deuxième pression, et
    • la séparation du premier composant gazeux du deuxième composant gazeux condensé dans le troisième dispositif de liquéfaction.
  4. Procédé selon l'une des revendications précédentes,
    le mélange gazeux (110) étant obtenu par une combustion d'oxyfuel.
EP08014024.7A 2008-08-05 2008-08-05 Séparation des gaz par condensation en plusieurs étapes Not-in-force EP2153879B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP08014024.7A EP2153879B1 (fr) 2008-08-05 2008-08-05 Séparation des gaz par condensation en plusieurs étapes

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP08014024.7A EP2153879B1 (fr) 2008-08-05 2008-08-05 Séparation des gaz par condensation en plusieurs étapes

Publications (2)

Publication Number Publication Date
EP2153879A1 EP2153879A1 (fr) 2010-02-17
EP2153879B1 true EP2153879B1 (fr) 2013-07-17

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Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1347558A (fr) * 1963-02-18 1963-12-27 Leybold Hochvakuum Anlagen Procédé et dispositif pour la récupération des constituants volatils pendant la dessiccation par congélation
US3349571A (en) * 1966-01-14 1967-10-31 Chemical Construction Corp Removal of carbon dioxide from synthesis gas using spearated products to cool external refrigeration cycle
DE4313574A1 (de) * 1993-04-26 1994-10-27 Leobersdorfer Maschf Verfahren zur Abscheidung von Kondensat aus Hochdruckluft
DE10245042B4 (de) * 2002-09-26 2007-09-27 DRäGER AEROSPACE GMBH Vorrichtung zur Anreicherung von Luft Sauerstoff
RU2272973C1 (ru) * 2004-09-24 2006-03-27 Салават Зайнетдинович Имаев Способ низкотемпературной сепарации газа (варианты)

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